US4071541A - Epoxidation - Google Patents

Epoxidation Download PDF

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Publication number
US4071541A
US4071541A US05/649,747 US64974776A US4071541A US 4071541 A US4071541 A US 4071541A US 64974776 A US64974776 A US 64974776A US 4071541 A US4071541 A US 4071541A
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United States
Prior art keywords
acid
process according
alkene
hydrogen peroxide
peracid
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Expired - Lifetime
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US05/649,747
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English (en)
Inventor
Anthony MacDonald Hildon
Peter Frederick Greenhalgh
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Solvay Interox Ltd
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Interox Chemicals Ltd
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Publication date
Application filed by Interox Chemicals Ltd filed Critical Interox Chemicals Ltd
Priority to US05/806,597 priority Critical patent/US4168274A/en
Priority to US05/806,944 priority patent/US4177196A/en
Priority to US05/823,696 priority patent/US4172840A/en
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Publication of US4071541A publication Critical patent/US4071541A/en
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D301/00—Preparation of oxiranes
    • C07D301/02—Synthesis of the oxirane ring
    • C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
    • C07D301/14—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with organic peracids, or salts, anhydrides or esters thereof
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C407/00—Preparation of peroxy compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C407/00—Preparation of peroxy compounds
    • C07C407/003—Separation; Purification; Stabilisation; Use of additives
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C409/00—Peroxy compounds
    • C07C409/24—Peroxy compounds the —O—O— group being bound between a >C=O group and hydrogen, i.e. peroxy acids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C409/00—Peroxy compounds
    • C07C409/24—Peroxy compounds the —O—O— group being bound between a >C=O group and hydrogen, i.e. peroxy acids
    • C07C409/26—Peracetic acid

Definitions

  • the present invention relates to the epoxidation of alkenes and more specifically lower alkenes.
  • alkene is used herein to mean the monounsaturated compounds and to include substituted compounds where the substitution will not prevent epoxidation.
  • the epoxidation reaction with which the present invention is concerned makes use of a peracid (otherwise known as a "peroxycarboxylic acid”).
  • a peracid otherwise known as a "peroxycarboxylic acid”
  • the product of the epoxidation reaction is called an "oxirane” or "epoxide”.
  • the present invention can be applied to ethylene, the lowest alkene, it is not thought that the reaction would be economically attractive at the present time as compared with the direct oxidation of ethylene. It would appear that the invention is likely to prove most advantageous when applied to propylene and chlor- or hydroxyl- substituted propylene.
  • Propylene is otherwise known as propene; the chloro-substituted compound is allyl chloride or 3-chloro-propene and the hydroxyl-substituted compound is allyl alcohol or 2-propen-1-ol.
  • propene will be used to include these substituted compounds and the terms "propylene", “allyl chloride” and “allyl alcohol” will refer to the specific compounds. It will be apparent that the corresponding oxiranes are epoxypropane, propylene oxide, epichlorhydrin and glycidol.
  • butene is intended to include both straight and branched chain isomers and internal and external olefins together with their substituted compounds.
  • the invention can also be applied to the various pentenes and to higher alkenes.
  • peracetic acid can be used in solution in acetic acid, optionally in admixture with acetone or methylal.
  • peracetic or perpropionic acid show marked advantages over perbutyric or performic acid, the latter being suggested in U.K. Pat. No. 1188791.
  • anhydrous perpropionic acid in the production of chloroepoxides is disclosed in U.K. Pat. No. 784620.
  • U.K. Pat. No. 1188791 also deals with the production of performic acid using an inert solvent, but it has not been suggested that a similar process can be applied to the production of perpropionic acid.
  • a process for epoxidation of an alkene by reaction with a peracid characterised by supplying an aqueous phase comprising sulphuric acid, hydrogen peroxide and water and an organic phase comprising acetic acid or propionic acid in a chlorinated hydrocarbon solvent to a liquid-liquid extraction device in such manner that these two phases pass in countercurrent through the extraction device; withdrawing from such extraction device an organic solution of peracid and carboxylic acid in the chlorinated hydrocarbon; passing said organic solution and the alkene cocurrently to a reactor; withdrawing from the reactor a product mixture and effecting fractional distillation thereof; withdrawing from such fractional distillation a product phase comprising the oxirane and a recycle phase comprising carboxylic acid in the chlorinated hydrocarbon, and passing such recycle phase from the distillation to the extraction device to form the organic phase therein.
  • chlorinated hydrocarbon Although the broad term "chlorinated hydrocarbon" is used herein, it should be understood that there are many practical constraints on the solvent which can be used. Thus the solvent must be non-reactive to all the other components of the system and must be readily separable from the product and recoverable from the various waste stream.
  • chlorinated hydrocarbons other than propylene dichloride it will be necessary to make appropriate adjustments to the concentrations of the other components in the system to secure proper operation and it may also be necessary to compensate for the altered physical equilibria by physical modification of the apparatus. For the sake of simplicity, only the use of propylene dichloride will be described.
  • Either acetic acid or propionic acid can be used as the carboxylic acid.
  • propionic acid to produce propylene oxide or epichlorhydrin and acetic acid to produce glycidol.
  • an aqueous phase is supplied to the extraction device, e.g. the upper part of an extraction column, to pass downwardly therethrough.
  • This aqueous phase comprises sulphuric acid, hydrogen peroxide and water.
  • the proportion of sulphuric acid is preferably approximately 45% by weight and is desirably between 30% and 60% by weight. If a lower yield is acceptable then the proportion of sulphuric acid can be between 15% and 85%.
  • the sulphuric acid is derived from 75% by weight sulphuric acid solution in water which forms a feedback from the purification stages which will be described hereinafter, together with make-up acid.
  • the hydrogen peroxide is conveniently approximately 28% by weight of the aqueous phase and in practice between 10% and 35% is very satisfactory. If lower yields are acceptable, then as little as 5% could be used, but above about 35% the mixture could be hazardous.
  • This hydrogen peroxide is of course a fresh reactant and is not a recycle stream and is very conveniently supplied as approximately 70% by weight solution in water. Water makes up the third component of the aqueous phase and its proportions can readily be found by difference.
  • the organic phase is fed into the lower part of the extraction column to pass upwardly in countercurrent with the aqueous phase and comprises, in the production of propylene oxide, a solution of propionic acid in propylene dichloride.
  • the concentration of propionic acid is preferably between 15% amd 30% of the organic phase or conveniently between 10% and 50% by weight.
  • the sulphuric acid performs the dual function of adjusting the specific gravity of the aqueous phase and adjusting the rate of the reaction between hydrogen peroxide and propionic acid to form perpropionic acid in perference to other competing reactions.
  • the function of the propylene dichloride is to extract the perpropionic acid from the aqueous phase in which it is formed by reaction between the hydrogen peroxide and propionic acid extracted from the organic phase into the aqueous phase.
  • the net result of the operation is to shift the equilibrium in favour of formation of perpropionic acid.
  • the solution of perpropionic acid in propylene dichloride from the extraction column is mixed with a molar excess, conveniently of the order of 25% to 50% (although it could be lower or higher) of alkene, e.g. propene, and is then pumped to a suitable reactor, e.g. a pressurised water-cooled tubular reactor.
  • a suitable reactor e.g. a pressurised water-cooled tubular reactor.
  • the degree of water cooling is desirably adjusted so as to provide a preferred temperature of about 100° C. If longer residence times or lower yields are acceptable, temperatures in the range 50° - 150° C could be used, but we prefer to operate in the range 75° - 120° C and desirably in the range 90° - 100° C.
  • the pressurisation is sufficient to maintain the propene safely in solution at the chosen temperature. If an adequate residence time is allowed in this reactor, for example in excess of 20 minutes and conveniently about 25 minutes in the manufacture of propylene oxide, but depending on temperature, very nearly complete conversion of the perpropionic acid will be achieved and conversions of approximately 99% based on the perpropionic acid can be achieved, with a yield of propylene oxide on perpropionic acid consumed in excess of 98%. It will be understood that with yields of this order, only very small amounts of side reactions take place, the most common being the degradation of perpropionic acid into propionic acid and oxygen or into ethanol and carbon dioxide. There is in addition formation of acetaldehyde, propionaldehyde, propylene glycol or propylene glycol esters and other side products but in general the sum of these do not exceed 2 mol % of the epoxide formed.
  • the product mixture from the reactor is taken to a multi-stage distillation process intended to separate out pure product, recycle streams and the impurities.
  • the precise details of the purification process will depend on the alkene and the relationship between its boiling point, that of the oxirane and the other constituents.
  • the product from the reactor is then conveniently subjected to a stripping operation in order to remove unreacted propylene and this propylene is recovered and recycled to the reactor.
  • the stripped product from the reactor is then suitable for separation by fractional distillation.
  • the light fraction comprises the propylene oxide, low boiling point impurities such as acetaldehyde, water and some propylene dichloride.
  • the heavy fraction from this first stage is propionic acid in propylene dichloride and this is recycled but may be distilled to remove heavy impurities such as propylene glycol.
  • the light fraction from the first stage is redistilled in a second stage to give a second light fraction comprising the propylene oxide, acetaldehyde and propionaldehyde and a second heavy fraction comprising water and propylene dichloride which is also recycled. Successive further distillations purify the propylene oxide.
  • the recycle phases can be passed back to the extraction column as the organic phase after the addition of perhaps minor amounts of propylene dichloride and propionic acid in order to make up for the small inevitable wastage and the purges.
  • the aqueous phase is supplied to the upper part of the column and is withdrawn from the lower part of the column.
  • the aqueous phase comprises sulphuric acid and water together with perhaps small amounts of hydrogen peroxide although as explained the conditions in the extraction column are preferably such as to ensure almost complete reaction of the hydrogen peroxide.
  • the second extraction will have removed substantially all the propionic and perpropionic acid from the aqueous effluent.
  • the dilute sulphuric acid is preferably concentrated, desirably by evaporation or distillation, in order to remove the unwanted water and then is recycled to the extraction column.
  • FIG. 1 is a flow sheet for the production of propylene oxide
  • FIG. 2 is a flow sheet for the production of epichlorhydrin.
  • the present invention being a continuous process, is best described with reference to the concentration of reactants flowing in various parts of the system.
  • the figures given correspond to a pilot scale operation but it will be readily understood by those skilled in the art how to scale up to any desired degree.
  • the plant comprises a three-section extraction column 10 to which is fed via an inlet 11 at the top of the centre section an aqueous phase comprising dilute sulphuric acid from recycle lines 12 and 13 and hydrogen peroxide from peroxide storage tank 14 via peroxide supply line 15.
  • the upper section of the column 10 functions as an acid backwash and for this purpose dilute sulphuric acid from the recycle line 12 is mixed with make-up acid from storage tank 16 supplied via line 17 and is fed by a line 18 to an inlet 19 at the top of the column 10.
  • an inlet 20 for an organic phase comprising a solution of propionic acid in propylene dichloride and this is supplied from organic storage tank 21 via line 22 and first organic recycle line 23.
  • the lower section of the extraction column 10 constitutes a stripper section and for this purpose is supplied with recycled propylene dichloride which is fed from a second organic recycle line 24 to an inlet 25 at the bottom of column 10.
  • An organic solution of perpropionic acid in propylene dichloride is withdrawn from the column 10 through line 26, is mixed with propylene supplied from propylene storage tank 27 via line 28 and is fed to a reactor 29.
  • reaction mixture is taken by line 30 to a stripping unit 31 in order to remove all traces of unreacted propylene.
  • the propylene is withdrawn from unit 31 through line 32 and a portion is passed to purge through line 33 and portion is pumped back through line 34 to join line 28.
  • the liquid from the stripping unit 31 is passed by a line 35 to a series of four distillation columns.
  • the heavy fraction is withdrawn through line 37 and passed to a solvent purification column 38.
  • the solvent mixture from line 37 is distilled in order to produce a light fraction which comprises a solution of propionic acid in propylene dichloride which is withdrawn from the column 38 through the line 23 previously referred to as the organic recycle line.
  • the heavy fraction from the solvent purification column 38 is passed to waste through line 39 as a purge. Some or all of the flow in line 37 can be passed directly to line 23, by-passing the purification column 38.
  • the light fraction from the distillation column 36 is taken by line 40 and passed to second distillation column 41.
  • the heavy fraction from the distillation column 41 is taken by a line 42 to a decanter 43 which separates out an aqueous phase which is passed to waste through line 44.
  • the organic phase from the decanter 43 is taken by the second organic recycle line 24 to be passed back to the extraction column 10.
  • the light fraction from the second distillation column 41 is taken by line 45 to the third distillation column 46 and this column is operated to withdraw a light fraction through a line 47 and pass it to waste. This fraction is in fact substantially acetaldehyde.
  • the heavy fraction from the distillation column 46 is taken by a line 48 and passed to the final distillation column 49 in which it is finally purified to give a heavy fraction which is withdrawn from the column through line 50 and passed to waste, this heavy fraction being substantially completely propionaldehyde.
  • the product is taken from the column 49 and passed to a propylene oxide storage vessel 51.
  • the aqueous phase therein passes out of the base of the column through a line 52 and a proportion is passed to purge through a line 53, this proportion constituting the acid purge.
  • the remainder in line 52 is passed to a distillation column 54 which serves to recover sulphuric acid.
  • the light fraction constitutes chiefly water and is passed to waste through line 55 whilst the heavy fraction constitutes recycle sulphuric acid and is withdrawn from the column 54 by the line 12 and is passed back to the extraction column 10 as previously described.
  • the plant to produce epichlorhydrin from allyl chloride is illustrated in FIG. 2 and it will be seen that it differs from that to produce propylene oxide chiefly in the purification stages.
  • the organic solution of perpropionic acid in line 26 is mixed with allyl chloride supplied from allyl chloride storage tank 60 via line 61 and is fed to the reactor 29.
  • reaction mixture is taken by line 62 to a fractionating column 63 which separates as a light fraction allyl chloride, propylene dichloride and water.
  • This light fraction passes through line 64 to a second fractionating column 65 where allyl chloride is separated as a light fraction and is withdrawn through line 66.
  • a portion of the allyl chloride in line 66 is passed to purge through line 67 and a portion is passed back through line 68 to joint line 61.
  • the heavy fraction from the second column 65 is taken by line 69 to a decanter 70 which separates out an aqueous phase which is passed to waste through line 71.
  • the organic phase from the decanter 70 is taken by line 72 and is split between the second organic recycle line 24 leading to the bottom of the extraction column 10 and a line 73 leading to a mixing device 74.
  • the heavy fraction from the first column 63 passes via line 75 to a distillation column 76.
  • the light fraction from the column 76 forms the product and is passed to a product storage tank 77, whilst the heavy fraction passes via line 78 to column 79.
  • the heavy fraction from the column 76 (mainly propionic acid) is distilled in order to produce a light fraction free of heavy impurities.
  • the heavy fraction from the column 79 is passed to waste through line 80 as a purge.
  • the light fraction from the column 79 is taken via a line 81 to the mixer device 74, where it is mixed with the solution from line 73 and passed into line 23, previously referred to as the organic recycle line.
  • the main inputs are hydrogen peroxide and propene (propylene or allyl chloride) with very minor make-up amounts of sulphuric acid, propionic acid and propylene dichloride.
  • the recycle streams and purge streams emphasize that under the conditions, the process of this invention produces the epoxide (propylene oxide or epichlorhydrin) at high yield and purity.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Epoxy Compounds (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
US05/649,747 1975-02-04 1976-01-16 Epoxidation Expired - Lifetime US4071541A (en)

Priority Applications (3)

Application Number Priority Date Filing Date Title
US05/806,597 US4168274A (en) 1975-02-04 1977-06-14 Production of a peracid and an oxirane
US05/806,944 US4177196A (en) 1976-01-16 1977-06-15 Epoxidation
US05/823,696 US4172840A (en) 1975-02-04 1977-08-11 Epoxidation

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB4692/75A GB1535313A (en) 1975-02-04 1975-02-04 Production of peracids and of epoxides
UK4692/75 1975-02-04

Related Child Applications (2)

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US05/806,597 Continuation-In-Part US4168274A (en) 1975-02-04 1977-06-14 Production of a peracid and an oxirane
US05/806,944 Continuation-In-Part US4177196A (en) 1976-01-16 1977-06-15 Epoxidation

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US4071541A true US4071541A (en) 1978-01-31

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US05/649,747 Expired - Lifetime US4071541A (en) 1975-02-04 1976-01-16 Epoxidation

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US (1) US4071541A (fr)
JP (1) JPS6025432B2 (fr)
AR (1) AR208107A1 (fr)
AT (1) AT356124B (fr)
AU (1) AU506647B2 (fr)
BE (1) BE838068A (fr)
BR (1) BR7600626A (fr)
CA (1) CA1070703A (fr)
CS (1) CS227653B2 (fr)
DD (1) DD122970A5 (fr)
DE (1) DE2602776C2 (fr)
DK (1) DK38776A (fr)
ES (1) ES444910A1 (fr)
FI (1) FI760167A (fr)
FR (3) FR2300085A1 (fr)
GB (1) GB1535313A (fr)
IE (1) IE42394B1 (fr)
IN (1) IN141031B (fr)
LU (1) LU74299A1 (fr)
NL (1) NL181579C (fr)
NO (1) NO148672C (fr)
PL (1) PL109648B1 (fr)
PT (1) PT64713B (fr)
RO (1) RO69626A (fr)
SE (1) SE424726B (fr)
SU (1) SU867307A3 (fr)
ZA (1) ZA76244B (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4172086A (en) * 1977-03-28 1979-10-23 Fmc Corporation Process for the manufacture of peroxycarboxylic acids
US4325888A (en) * 1978-01-13 1982-04-20 Propylox Preparation of peracid by liquid-liquid extraction
US4344897A (en) * 1978-12-29 1982-08-17 Bayer Aktiengesellschaft Process for the preparation of percarboxylic acid solutions
US4370251A (en) * 1980-07-25 1983-01-25 Fmc Corporation Continuous process for the production of peroxycarboxylic acid compositions
EP1773764A2 (fr) * 2004-07-28 2007-04-18 Peragen Systems, Inc. Procede continu destine a une production sur le site et sur demande d'acide peracetique aqueux

Families Citing this family (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS53105410A (en) * 1976-03-02 1978-09-13 Propylox Sa Process for preparing peracid
GB1584355A (en) * 1976-10-26 1981-02-11 Propylox Sa Epoxidation
GB1589066A (en) * 1977-02-26 1981-05-07 Propylox Sa Process for the production of peroxycarboxylic acids
DE2718602A1 (de) * 1977-04-22 1978-10-26 Kraftwerk Union Ag Vorrichtung zum spannen mehrerer schraubenbolzen
DE2734085A1 (de) * 1977-07-28 1979-02-22 Bayer Ag Verfahren zur herstellung von halogenalkylsubstituierten oxiranen
DE2734086A1 (de) * 1977-07-28 1979-02-22 Bayer Ag Verfahren zur herstellung von halogenalkylsubstituierten oxiranen
DE2734243A1 (de) * 1977-07-29 1979-02-08 Bayer Ag Verfahren zur herstellung von halogensubstituierten vinyloxiranen
DE2734240A1 (de) * 1977-07-29 1979-02-08 Bayer Ag Verfahren zur herstellung von vinyloxiran
DE2734242A1 (de) * 1977-07-29 1979-02-08 Bayer Ag Verfahren zur herstellung von vinyloxiran
FR2421168A1 (fr) * 1978-03-28 1979-10-26 Propylox Sa Procede pour la fabrication de peracides carboxyliques
DE2835884A1 (de) * 1978-08-16 1980-02-28 Bayer Ag Verfahren zur herstellung von 7-oxabicyclo(4.1.0)heptan-3,4-dicarbonsaeure-diglycidylester
DE2835886A1 (de) * 1978-08-16 1980-02-28 Bayer Ag Verfahren zur herstellung von glycidylestern aromatischer polycarbonsaeuren
DE2835882A1 (de) * 1978-08-16 1980-02-28 Bayer Ag Verfahren zur herstellung von fumarsaeureglycidylestern
DE2835885A1 (de) * 1978-08-16 1980-02-28 Bayer Ag Verfahren zur herstellung von 7-oxabicyclo(4.1.0)heptan-3,4-dicarbonsaeurediglycidylester
DE2835881A1 (de) * 1978-08-16 1980-02-28 Bayer Ag Verfahren zur herstellung von glycidylestern cycloaliphatischer polycarbonsaeuren
DE2835883A1 (de) * 1978-08-16 1980-02-28 Bayer Ag Verfahren zur herstellung von maleinsaeureglycidylestern
FR2455580A1 (fr) 1979-05-04 1980-11-28 Propylox Sa Procede pour l'epuration de solutions organiques de peracides carboxyliques
DE3049434A1 (de) * 1980-12-30 1982-07-29 Peroxid-Chemie GmbH, 8023 Höllriegelskreuth Verfahren zur herstellung von epoxiden
EP0056932B1 (fr) * 1981-01-15 1984-09-19 Bayer Ag Procédé de préparation et d'isolement de n-alkyloxirannes
FR2502620A1 (fr) * 1981-03-24 1982-10-01 Ugine Kuhlmann Procede continu de preparation de l'oxyde de propylene
JPS6357952U (fr) * 1986-10-01 1988-04-18
JP2022522277A (ja) * 2019-02-22 2022-04-15 ヌーリオン ケミカルズ インターナショナル ベスローテン フェノーツハップ 有機過酸化物を生成するためのプロセス

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2977374A (en) * 1961-03-28 Process for preparing oxirane
US3065246A (en) * 1962-11-20 Continuous epoxidation method
US3141896A (en) * 1964-07-21 Process for the percarboxylic acid epqxr
US3476776A (en) * 1964-10-22 1969-11-04 Knapsack Ag Process for the manufacture of alkane epoxides
GB1188791A (en) * 1966-04-14 1970-04-22 Laporte Chemical Olefin Oxides
US3708507A (en) * 1969-08-21 1973-01-02 Degussa Process for the epoxidation of unsaturated compounds
DE2141156A1 (de) * 1971-08-17 1973-03-01 Degussa Verfahren zur herstellung organischer percarbonsaeureloesungen
US3799949A (en) * 1970-12-08 1974-03-26 Degussa Process for the preparation of epichlorhydrin from allylchloride

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2977374A (en) * 1961-03-28 Process for preparing oxirane
US3065246A (en) * 1962-11-20 Continuous epoxidation method
US3141896A (en) * 1964-07-21 Process for the percarboxylic acid epqxr
US3476776A (en) * 1964-10-22 1969-11-04 Knapsack Ag Process for the manufacture of alkane epoxides
GB1188791A (en) * 1966-04-14 1970-04-22 Laporte Chemical Olefin Oxides
US3708507A (en) * 1969-08-21 1973-01-02 Degussa Process for the epoxidation of unsaturated compounds
US3799949A (en) * 1970-12-08 1974-03-26 Degussa Process for the preparation of epichlorhydrin from allylchloride
DE2141156A1 (de) * 1971-08-17 1973-03-01 Degussa Verfahren zur herstellung organischer percarbonsaeureloesungen

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4172086A (en) * 1977-03-28 1979-10-23 Fmc Corporation Process for the manufacture of peroxycarboxylic acids
US4325888A (en) * 1978-01-13 1982-04-20 Propylox Preparation of peracid by liquid-liquid extraction
US4344897A (en) * 1978-12-29 1982-08-17 Bayer Aktiengesellschaft Process for the preparation of percarboxylic acid solutions
US4370251A (en) * 1980-07-25 1983-01-25 Fmc Corporation Continuous process for the production of peroxycarboxylic acid compositions
EP1773764A2 (fr) * 2004-07-28 2007-04-18 Peragen Systems, Inc. Procede continu destine a une production sur le site et sur demande d'acide peracetique aqueux
EP1773764B1 (fr) * 2004-07-28 2012-10-31 Peragen Systems, Inc. Procede continu destine a une production sur le site et sur demande d'acide peracetique aqueux

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NL181579B (nl) 1987-04-16
GB1535313A (en) 1978-12-13
JPS6025432B2 (ja) 1985-06-18
FR2379520B1 (fr) 1981-06-26
CS227653B2 (en) 1984-05-14
ATA60976A (de) 1979-09-15
AU1033176A (en) 1977-07-21
ES444910A1 (es) 1977-04-16
SE7601146L (sv) 1976-08-05
FI760167A (fr) 1976-08-05
NL7601048A (nl) 1976-08-06
BE838068A (fr) 1976-07-30
DD122970A5 (de) 1976-11-12
IE42394L (en) 1976-08-04
NO148672B (no) 1983-08-15
DE2602776C2 (de) 1984-05-17
FR2379519A1 (fr) 1978-09-01
JPS51101906A (fr) 1976-09-08
FR2379520A1 (fr) 1978-09-01
RO69626A (fr) 1981-11-24
NL181579C (nl) 1987-09-16
SE424726B (sv) 1982-08-09
CA1070703A (fr) 1980-01-29
FR2300085A1 (fr) 1976-09-03
PT64713A (fr) 1976-02-01
NO148672C (no) 1983-11-23
ZA76244B (en) 1977-01-26
DK38776A (da) 1976-08-05
BR7600626A (pt) 1976-08-31
IN141031B (fr) 1977-01-15
AT356124B (de) 1980-04-10
PL109648B1 (en) 1980-06-30
DE2602776A1 (de) 1976-08-05
AU506647B2 (en) 1980-01-17
IE42394B1 (en) 1980-07-30
NO760310L (fr) 1976-08-05
AR208107A1 (es) 1976-11-30
LU74299A1 (fr) 1976-06-18
SU867307A3 (ru) 1981-09-23
FR2300085B1 (fr) 1980-10-03
FR2379519B1 (fr) 1980-10-31
PT64713B (fr) 1977-08-11

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